Method for distributing a vapor-liquid feed and apparatus therefor



Aug. 4, 1959 R. R. HALIK ET AL METHOD FOR DISTRIBUTING A VAPOR-LIQUIDFEED AND APPARATUS THEREFOR 3 Sheets-Sheet 1 Filed NOV. 5, 1957 4, 1959R. R. HALIK ETAL 2,898,292

METHOD FOR DISTRIBUTING A VAPOR-LIQUID FEED AND APPARATUS THEREFOR FiledNov. 5, 1957 I5 Sheets-Sheet 2 I 2 n n i E 1 5 v INVENT R5 BY DwlM-"jfii ATTORNEY R. R. HALIK ETAL METHOD FOR DISTRIBUTING A VAPOR-LIQUID-Aug. 4, 1959 FEED AND APPARATUS THEREFOR 3 Sheets-Sheet 3 Filed Novv 5.1957 I'I'I'I'I'IIA Fig.1).

ATTORNEY United States P tent 2,898,292 METHOD FOR A VAPOR-LIQUID FEEDAND APPARATUS THEREFOR Raymond R. Hal ik, Pitman, and Donald F. Hill,West Dptford Township, Gloucester County, N ..l., assignors toSoconyMobil Oil Company, Inc., a corporation of New York Application November1957, Serial No. 694,621

12 Claims. (Cl. 208-450 The present invent-ion'relates re means fordistributing ateed to a reactor which feed comprises a liquid portionand a vaporous and/or gaseous portion. Thus, for ex ample, whenhydrodesulfurizingpet'roleumfractions boiling above the gasoline boilingrange, i.e., having an initial b'oiling'point of about 400 to "about 450F at temperatures of about 600 to about 800 F. and 'at pressures of 1-00to about 500 ip.s;i.g., a portion of the normally liquid hydrocarbonfraction is in the vapor state. Consequently, the introduction of a feedwhich is mixed phase, i.e., partly in the vapor phase and partly in theliquid phase, presents a problem. Furthermore, since it isgenerally'accepted by thoseskilled in the art that the hydro- .geri forthe de'sulfurization reaction should be intimately mixed with the feed,a further problem is encountered.

A distributor meeting the requirements for distributing a mixed phasefeed uniformly over the cross-section of a bed of catalyst must deliverthe mixed phase feed in a manner to minimize hydraulic gradient effects.The distributor must also be capable of operating in a satisfactorymanner although the volume of the petroleum fraction introduced per unitof time is subject to wide fluctuations.

It has been found that the use of inert pellets, preferably spheres, tosupplement the distribution of the feed by the distributing means of thepresent invention improves the distribution pattern through the bed ofcatalyst. The layer of inert, i.e., chemically inert, spheres or likeparticles, provides additional intimate mixing of the hydrogen with theliquid prior to reaction. Furthermore, a layer of inert spheres preventsboiling or disturbance of the catalyst bed. It is particularly desirableto prevent dishing or hollowing-out of the center of thecatalyst bed.Dishing or hollowing-out of the center of the catalyst bed causes theflow of liquid to the center of the bed which results in a poor liquiddistribution pattern within the bed.

The problems attendant upon the feeding of a mixed phase material (amaterial partially in the liquid phase and partially in the vapor phaseat the temperature and pressure existing in the reaction zone) have beensolved in the manner illustrated in the drawings. In general, thepresent invention includes a primary distributor constructed andarranged to provide for disengaging the vapor portion of the feed fromthe liquid portion of the feed while also providing a quietnon-turbulent flow of "the liquid portion of the mixed phase feed fromthe inlet pipe or pipes" to the outlet nipples of the primardistributor. A secondary distributor constructed and arranged todistribute the mixed phase fe'ed uniformly over the cross-section of thecatalyst bed is also provided in several embodiments of the presentinvention. In con junction with the primary andsecondary distributor alayer of chemically inert spherical pellets or the like is interposedbetween the distributor and the upper surface of thejcatalystbeda Thoseskilled in' the art will have a better understanding of the presentinvention from the following descrip- 2,898,292 Patented Aug; 4, 1959 2tion taken in conjunction with the drawings in which the same numbersrefer to similar parts and in 'Which Figure 1 is a vertical section of'areactor;

Figure 2 is a plan view of a secondary distributor at line 22 of Figure1;

Figure 3 is a side elevation ofa feed box of the'primary distributorshown in Figures 1 and 2;

Figure 3a is an end elevation of the feed box shown in Figure 3; I IFigure 4 is a vertical section of a downcornei' shown in Figures 1 and2; p t

Figure 5 is a vertical section of a reactorshowing 'a primarydistributor and secondary'distributor of the present invention andomitting the catalyst bed and the superposed layer of inert pellets forsimplicity;

Figure 6 is a plan view of the reactor shown iii sectidh in Figure 5;

Figure 7 is a vertical section of a reactor showiiig primary andsecondary distributor of'the present invention and omitting the catalystbed and the superposed layer of inert pellets for simplicity; v

Figure 8 is a plan view of the primary distributor of Figure 7; V

Figure 9 is a vertical section of a reactor omitting the catalyst bedand superposed layer of inert pellets and showing primary and secondarydistributors of the present invention; V

4 Figure 10 is a plan View of the primary distributor of Figure i Figure11 is a plan view of a secondary distributor showing the distributornipples in only onequadrant of the plate for simplicity; and

Figure 12 is a vertical section or anenlarged secondary distributornipple. t a v I Referring to Figure 1; a cylindrical r'eactor shellsuitably insulated for the temperatures employed and preferablyresistant to co'r'r'osio'ri is provided with a tap 2 and a bottom 3.Bottom 3 is provided with an dutlet conduit 4. Concentric with thevertical axis efeuflet' 4 reactor 1 is provided with aforaminoussolids-fiuids' sa ara'tor 5. The catalyst particles arewithheld from en'- tering chamber 5 by any suitable means. Thiscaricomprise a perforated plate 6 supported by channels 7. Piererably,this plate 6 can be omitted and the lower chamber of the reactor 8 canbe filled with inert materials such as- Mull ite or Alundum pellets orsph res; A distributor plate 9 is rigidly mounted in any suitablerii'arni'er in reactor 1 vertically spaced from perforated plate 6 adistance to provide for a bed of particle-form solid goat alyst ofrequired depth and a superposed la er of inert pellets, such as"Mull'iteor Alundun'izl Distributor plate 9 is rigidly'moun'ted in reactor 1 andsupportedin any suitable manner as by angles 10 and channels not shown.Distributor plate'9 must be mounted substantially horizontally, i.e. thevariation from the true horizontal must not be more than about /i-'inch'for'a reactor 6 feet in diameter. 7

In the embodiment of the present invention illustrated in Figure 1 thesecondary distributor consists of a fplu ra-lity of distributor channelsor boxes 11 suppo ed by secondary distributor plate 9. Eachof'thedistributor channels or boxes isprovided with" at least one inlet12. The construction of distributor channels l'l 'is readily understoodby reference to Figures 3 and 3a. Inspection of Figure 3 makes it"manifest that box or channel 1 1 has longitudinal sides which are cutaway to leave a central portion 13 flanking the inlet 12 so that the in;coming mixed phase or liquid phase feed cannot now laterally of theinlet but must flow longitudinally a distance sufiicient to permit theflow to become non-turbiF lent. Preferably, central portion or baffle 13rests upon secondary distributor plate 9 or at least is in closeproxirnity thereof, say about 0.25 inch maximum. End 14 of channel orbox 11 is provided with a skirt covering approximately the upperone-half area and leaving an opening 15 under the liquid surface asillustrated in Figure 3a. The distance from the plate 9 to the top ofchannel 11 is preferably equal to or slightly greater than the depth ofliquid during operation.

Reactor 1 is provided with an inlet 16 having closure flange l7 andmatching closure plate 18. Closure plate 18 preferably is provided withone or more gas inlets 19 constructed and arranged to deliver the gas ina direction parallel or perpendicular to the plane of distributor plate9. Closure plate 18 is also provided with a liquid phase or mixed phasefeed inlet 20 connecting with vapor-liquid tight inlet box 21. Inlet boxor primary distributor 21 is provided with a plurality of outlets 22.These outlets are so sized or provided with inlet orifices to providesubstantially uniform flow to each pipe 24. Inlet box outlets 22 anddistributor channel inlets 12 are connected in a vaporand fluid-tightmanner as by pipes 24 so that the feed introduced into inlet box 21flows to channels 11. To support distributor plate 9 and increase therigidity thereof distributor plate 9 is provided with ribs 23. Ribs 23also act to make the flow of liquid across distributor plate lessturbulent. Distributor plate 9 is provided with a plurality of outletnipples 25 having a plurality of serrations or notches 26 equally spacedon the circumference of the outlet nipple. (See Fig. 4.)

Mixed phase feed flows to the reactor inlet 20, thence to primarydistributor 21. From inlet box 21 the mixed phase feed flows throughprimary distributor outlets 22, conduits or pipes 24 and channel inlets12 to distributor channels or boxes 11. From distributor channels orboxes 11 the mixed phase feed flows over distributor plate 9 until thedepth of the liquid on plate 9 is somewhat greater than the height ofthe bottoms'of the notches 26 in distributor plate outlets 25. Theactual liquid level will increase or decrease as the flow rate to thereactor--and thus to each downcomer-is increased or decreased. Thedistributor plate outlet nipples 25 are distributed substantially asshown in Figure 2. The liquid and vapor flow downwardly throughdistributor plate nipples 25. The contact of vapors with liquid in theconcurrent flow through the nipples 25 and especially through the inertlayer 27 intimately mixes the vapors and liquid prior to their entryinto the catalyst bed.

The liquid feed, vaporous feed and hydrogen gas flow downwardly throughthe layer of inert pellets 27. While the primary and secondarydistributors are of primary importance in establishing uniformdistribution of feed over the cross-section of the catalyst bed 28, thelayer of inert pellets contributes to further equalize any nonuniformitywhich may exist. The mixed phase hydrocarbon feed and hydrogen flowsdownwardly through the layer of inert pellets, and the bed ofparticle-form solid catalyst to fiow from the reactor throughliquid-vaporsolids separator and thence to 'reactor outlet 4 tofractionating and other finishing processes. can be spaced a negligibledistance from solids-liquidvapor separator 5, it is preferred to omitspace plate 6 and support the bed of catalyst on a bed of inert pelletsfilling the lower section of the reactor. When plenum 8 is filled withinerts, plate 6 may be omitted with no ill effect on the operation.

Referring now to Figures 5 and 6; reactor 31 suitably lined to resistcorrosion and preferably insulated is proyided with secondarydistributor plate 9 similar in construction and arrangement todistributor plate 9 (Figure l) and having distributor plate nipplesconstructed and arranged as distributor plate nipples 25 (Figure l).Distributor plate 9 is supported and strengthened by angles and ribs asmore fully discussed in the de scription of Figures 1 and 2. Reactor 31is provided with a flange 17 and closure plate 18 similar to those Whileplate 6 t described in conjunction with Figure 1. Reactor 31 is alsoprovided with a vapor-solids separator similar to that (5) described inthe discussion of Figures 1 and 2 and with a liquid products outletsimilar to that (4) described in the discussion of Figures 1 and 2.

Primary distributor 21 is a box-like structure open at the top to thereactor and provided with a plurality of outlets 22 in the bottomthereof. The secondary distributor comprises plate 9 and nipples ordowncomers 25 similar in size and distribution to plate 9 and nipples 25in Figures 1 and 2 or distributed as are downcomers 25 in Figure 12. Theboxes 11 are similar in construction and purpose to boxes 11 in Figures1, 2 and 3. Boxes 11 and outlets 22 are connected in any suitable mannerbymeans of conduits 12.

The mixed phase feed flows into primary distributor box 21 through inlet20 which is a conduit of suitable size to permit free flow of the volumeof feed charged. The outlet of conduit 20 is in the vicinity of thebottom of box 21. The mixed phase feed enters box 21, the vapors aredisengaged in box 21, the liquid portion of the feed flows from box 21through outlets 22 and conduits 12 to discharge boxes 11. From dischargechannels 11 the liquid flows non-turbulently to the downcomers 25 insecondary distributor 9. The liquid portion of the feed flows downwardlythrough downcomers 25 together with the vaporous portion of the feed andany additional gaseous reactant which can be introduced into the reactorthrough separate inlets 19. Secondary distributor 9 spreads the feedover the cross-section of the layer of chemically inert pellets(preferably spheres) which improves the substantially uniformdistribution of the feed produced by the primary and secondarydistributors. Those skilled in the 'art will understand that there is anegligible pressure differential between the space above plate 9 and thespace below plate 9.

Referring now to Figures 7 and 8; the mixed phase feed is introducedinto the primary distributor 21 through conduit 20. The gaseousreactant, when introduced separately, enters the reactor through one ormore pipes 19. The secondary distributor is similar in construction andarrangement of downcomers 25 and ribs 23 to the secondary distributorsof Figures 1, 2, 5, 11, and 12. However, in the embodiment of thepresent invention illustrated in Figures 7 and 8 the primarydistributor, while serving the same purpose of disengaging the vaporousportion of the mixed phase feed and delivering the liquid portion of themixed phase feed to the secondary distributor is of somewhat differentconstruction.

Primary distributor 21 comprises a box, preferably circular, preferablyconcentric with conduit 20, which rests upon and is supported bysecondary distributor plate 9. Primary distributor 21 preferably isconstructed as a large conduit having plate 30 mounted in asubstantially liquid-tight manner a short distance upwardly from thebottom 0f the conduit. The upper edge of this box 21 may be smooth asshown or provided with a multiplicity of notches. A second conduit 31 ismounted in a substantially liquid-tight manner concentric with conduit20 on plate 30. Below the plane of plate 30 the periphery of conduit orbox 21 is provided with a plurality of notches 32 of suflicient size andnumber to provide non-turbulent flow of liquid to the downcomers 25within the periphery of conduit or box 21. The tops of the notches 32are somewhat above the liquid phase at the tops of downcomers 25.

The flow of feed is as follows: The mixed-phase feed flows throughconduit 20 into internal conduit or weir 31. At least a portion of thevapors of the mixed phase feed is disengaged within conduit or weir 31.The liquid portion of the feed and entrained vapors flow over the top ofprimary weir 31 into the annulus or weir 21. In annulus 21 thedisengagement of the vaporous portion of the feed is substantiallycompleted and the liquid portion of ,the feed flowsin a non-turbulentmanner over the top ofweir 21 on to secondary distributor plate 9.

Secondary distributor plate 9 is similar in' construction andarrangement of downcomers to plates 9 in Fig .ures 2 and 11. The liquid,disengaged vapors and gaseous reactant, if any, flow in non-turbulentmanner through downcomers 25 in distributor plate 9 including thosewithin the area immediately beneath primary distributor 21. The liquidfeed, the vapor feed and the gaseous reactant, if any, flow downwardlythrough downcomers. 25 onto the surface of a layer of chemically inertpellets which further improve the distribution of the mixed ,phase feedand gaseous reactant, if any, over the cross- :section of the catalystbed beneath the layer of inert ,pellets.

In'Figures 9 and I is-illustrated another embodiment of the presentinvention. ,-A primary distributor box 21 having a circular, hexagonal,or other suitable shape 'is provided with a plurality of downcomers 32near the periphery of .the box distributed in 'apattern similar to thatshown in Figure 10. Downcomers 32 :arenipples provided with :slotseither V-shaped or rectangularshaped with the bottom of the notchappreciably above the outlet edge of conduit 20 to provide non-turbulentflow without hydraulic gradient from'conduit 20 over the surface of box21. The 'outlet ends of downcomers 32 are slotted similarlyv to providenon-turbulent flow of liquid from downcomers 32 to downcomers 25 insecondary distribution plate -9. Those skilled in the art willunderstand that at least a portion of the vaporous component of themixed phase feed is disengaged as the mixed phase feed flows-fromconduit20 to downcomers 32 "and that the balance of the vaporous portion of themixed phase feed is disengaged when the feed flows from downcomers 32 todowncomers 25 in non-turbulent-manner. As in the other embodiments ofthe present invention the liquid component flows from secondarydistribution plate 9 downwardly through downcomers 25 onto-a layer ofinert pellets resting on thetop of the bed of particle-form catalyst.'Due to the negligible pressure differential between the space underplate 9 and above plate 9 the vaporous component of the mixed phase feedand the gaseous reactant, if any, flow concurrently with the liquidcomponent of the mixed phase feed downwardly through-downcomers 25 ontoand throughthe layer of inert pellets and the bed of particle-formcatalyst.

"Thesize and distribution of downcomers'in' secondary distribution plate9 is important. Each downcomer pipe in-the secondary distributor shouldfeed a catalyst bed area of not less than about 0.1 square foot (roughly-4 inch diameter) and not more than about 1.0 square foot (14 inchdiameter). Coverage ofan area smaller than 0.1 square foot is notpractical since tray area is almost completely filled at this spacingand there would be only slight gain in distribution. An area-coveragegreater than 1.0 square foot would result in a large loss 'of catalystvolume. This is due to the fact that liquid issuing from a downcomerpipe must spread out as the flow moves downward through the bed.Therefore, increasing the area of each downcomer also increases the beddepth required before the liquid fans out to cover the entirecross-section of the bed. In general, the preferred coverage, withintheabove-mentioned range, would be downcomers spaced every 8 to 10 inchesapart.

The preferred design features for each downcomer discharging liquid andgas to .the catalyst bed are:

(l) The downcomer-pipe diameter should preferably be at least percentand not more than about 50 percent of the diameter for thearea eachdowncomer-feeds. (In our commercial and laboratory designs, 2'' diameterdowncomers were spaced 8 to 9 inches apart, or a downcomer diameterequal to 22 percent to 25 percent of the diameter for the bed areacovered by each downcomer.)

(2) At the same time, the downcomer diameter where V =total volume ofliquid per second at operating conditions, ftfi/sec.

"V,=total volume of vapor per second at operating conditions, .ft. sec.A=cross sectional area of each downcomer, ft.

N=total number of downcomers Superficial velocities of less than about30 feet per secondprovide satisfactory results.

.It may be desirable to provide two or more sizes of downcomer pipes onthe primary distributor tray. For example, in a cylindrical vessel asshown in Figure l, a standard pattern or arrangement of downcomers willleave unwetted areas in the catalyst bed near the periphery.Consequently, somewhat smaller downcomers, than used on the rest of thetray, may be used to fill in these spaces to completely wet the bed.

If the liquid phase is introducedon to the secondary distributor tray insuch a'manner that a hydraulic gradient exists across the secondarytray, 'maldistribution will :occur. To minimize the hydraulic gradient,devices previously described for distributing the liquid to thesecondary downcomertray are recommended. Preferably, these devices wouldlimit the hydraulic gradient between any two points on the secondarydistributor tray toless than about M".

We claim:

.1. A method of distributing a mixed phase-feed uniformly over thecross-section of a bed of particle-form material confined in a reactorwhich comprises introducing a mixed phase feed comprising a vaporouscomponent and a liquid component into a reactor at a point spacedvertically from the top of a bed of particle-form material, disengagingat least aportion of said vaporous component whilst subjecting saidliquid component to non-turbulent flow through a distributing zonespaced above, concentric with, and having substantially thesamecross-sectional area as said bed of particle-form material, flowing saidliquid component from said distributing zone as a plurality of streamsdownwardly onto the upper surface of said bed of particle-form material,each of said plurality of streams having a superficial velocitynotexceeding 30 feet per second and flowing said disengaged vaporouscomponent through the aforesaid bed of particle-form material inintimate association with said liquid component.

2. The method of distributing a mixed phase feed uniformly over thecross-section of a bed'of particle-form material comprising a catalystas set forth and described in claim 1 wherein the plurality of streamseach having a'superficial velocity not exceeding 30 feet per second flowonto and through a layer of inert pellets, and the multiplicity ofstreams of liquid component produced inssaid2layer of inert pellets'flowonto andthrough'said bed .ofparticle-form catalyst.

.3. The method of distributing a mixed phase feed uniformly overthecross-section of a bed of particle- 'form material comprising acatalyst as set forth anddescribed in claim 1 wherein the plurality ofstreams each having a superficial velocity not exceeding 30 feet persecond flow onto and through a layer of inert substantially sphericalpellets, and the multiplicity of streams of liquid component produced insaid layer of inert sub- 7 stantially spherical pellets flow onto andthrough said bed of particle-form catalyst.

4. An apparatus for distributing a mixed phase feed comprising avaporous component and a liquid component uniformly over a bed ofparticle-form solid ma- ,terial which comprises a closed container, amixed feed inlet, an outlet, a bed of particle-form solid material inthe lower region of said container, a secondary distributor verticallyspaced upwardly from said bed of particle-form material constructed andarranged to provide a plurality of downwardly extending conduits in theratio of one conduit for each 0.1 to not more than about ,1.0 squarefoot of horizontal cross-sectional area of said bed of particle-formsolid material, a primary distributor constructed and arranged todeliver in substantially nonturbulent flow to said secondary distributorsaid liquid component whilst disengaging at least a portion of saidvaporous component of said mixed phase feed, and means for introducingsaid mixed phase feed to said primary distributor. i

5. In the apparatus described and set forth in claim '4 a mass ofsubstantially inert material interposed between said catalyst bed andsaid secondary distributor, said mass of substantially inert materialbeing provided with a multiplicity of interconnected fissures providing'a multiplicity of tortuous paths from the side of said mass facing saidsecondary distributor through said mass of substantially inert materialto the side of said mass facing said catalyst bed. 6. An apparatus fordistributing a mixed phase feed comprising a vaporous component and aliquid component uniformly over the cross-section of a bed ofparticle-form solid material which comprises in a closed containerhaving a mixed phase feed inlet located in the region of the topthereof, a products outlet in the region of the bottom of saidcontainer, and a bed of particle-form solid material therein interposedbetween said mixed feed inlet and said products-outlet, said bed ofparticle-form solid material having the bottom thereof contiguous'tosaid products outlet and having the top thereof spaced downwardly fromsaid mixed phase feed inlet, said bed of particle-form solid materialhaving a cross-section substantially that of said container, a sec-.ondary distributor comprising a plate mounted horizontally in aliquidand gas-tight manner to provide substantially no hydraulicgradient horizontally to said plate and provided with a plurality ofconduits in the ratio of one conduit per 0.1 to about 1.0 square foot ofhorizontal cross-sectional area of said bed of particle-form solidmaterial, a primary distributor mounted horizontally in spaced relationabove said secondary distributor comprising a tray and a plurality ofconduits mounted in said tray, the lower portions of said conduits beingnotched and contiguous to said horizontal plate of said secondarydistributor to provide substantially nonr turbulent flow of liquidcomponent of said mixed phase feed over said horizontal plate of saidsecondary distributor whilst disengaging the vaporous component of saidmixed phase feed, the upper portions of said conduits being notched, thesides of said tray extending j mass of substantially inert materialbeing provided with a multiplicity of interconnected channels providingamultiplicity of tortuous paths from the side of said mass ofsubstantially inert material facing said secondary distributor throughsaid mass of substantially inert material to the side of said mass ofsubstantially inert material facing said bed of particle-form material.

8. In the apparatus for distributing a mixed phase feed over a bed ofparticle-form solid material as'set forth and described in claim 4wherein the primary dis- .tributor comprises a first conduit interposedbetween the horizontal plate of thesecondary distributor aud'the :meansfor delivering mixed phase feed to said primary distributor, the lowerend of said conduit being notched and contiguous to'said horizontalplate, a horizontal plate mounted in a liquidand gas-tight manner ins'aid conduit above theupper edges of saidnotches, and a second conduitmounted vertically in a liquid and "gastight manner within said firstconduit on said horizon.- tal plate, the upper edge of said secondconduit being in .a plane above the plane of said first conduit, saidsecond conduit being concentric with said means for delivering mixedphase feed to said primary distributor. 1

9. In the apparatus for distributing a mixed phase feed over a bed ofparticle-form solid material as set forth and described in claim 4wherein the primary distributor comprises a tray concentric with themeans for delivering mixed phase feed to said primary distributor andinterposed between said mixed phase delivery means and said secondarydistributing means, a plurality of partially closed end channels havingthe open side contiguous to said secondary distributor constructed andarranged to provide non-turbulent flow of liquid component -whilstdisengaging vaporous componentof said mixed phase feed, and meansconnecting said tray and said channels. 10. In the apparatus fordistributing a mixed pha feed over a bed of particle-form solid materialasset forth and described in claim 4 wherein the-primary distributorcomprises a plurality of partially closed end channels having the openside contiguous 'to said secondary distributor constructed and arrangedto provide non-turbulent flow of liquid component whilst disengagingvaporous component of said mixed phase feed, and a plurality of conduitsconnecting said mixed phase feed inlet with said plurality of closed endchannels.

11. Inthe apparatus for distributing a mixed phase feed as described andset forth in claim 4 means for introducing gaseous reactant separatelyinto said container. I

12. In the apparatus for distributing a mixed phase feed over a bed ofparticle-form solid material as set forth and described in claim 4wherein the primary distributor comprises a tray concentric with themeans'for delivering mixed phase feed to said primary distributor andinterposed between said mixed phase feed delivery means and saidsecondary distributing means, a plurality of partially closed endchannels having the open sides contiguous to said secondary distributor,trapezoidal baffle mounted substantially in the plane of the open sidesand opposite each mixed phase feed delivery means with the shorterof-the two parallel sides of said baffle substantially in the plane ofthe lower edge of said partially closed ends. I

References Cited in the file of this patent UNITED STATES PATENTS "at v

1. A METHOD OF DISTRIBUTING A MIXTURE PHASE FEED UNIFORMLY OVER THECROSS-SECTION OF A BED PARTICLE-FORM MATERIAL CONFINED IN A REACTORWHICH COMPRISES INTRODUCING A MIXED PHASE FEED COMPRISING A VAPOROUSCOMPONENT AND A LIQUID COMPONENT INTO A REACTOR AT A POINT SPACEDVERTICALLY FROM THE TOP OF A BED OF PARTICLE-FORM MATERIAL, DISENGAGINGAT LEAST A PORTION OF SAID VAPOROUS COMPONENT WHILST SUBJECTING SAIDLIQUID COMPONENT TO NON-TURBULENT FLOW THROUGH A DISTRIBUTING ZONESPACED ABOVE, CONCENTRIC WITH, AND HAVING SUBSTANITALLY THE SAMECROSS-SECTIONAL AREA AS SAID BED OF PARTICLE-FORM MATERIAL FLOWING SAIDLIQUID COMPONENT FROM SAID DISTRIBUTING ZONE AS A PLURALITY OF STREAMSDOWNWARDLY ONTO THE UPPER SURFACE OF SAID BED OF PARTICLE-FORM MATERIAL,EACH OF SAID PLURALITY OD STREAMS HAVING A SUPERFICIAL VELOCITY NOTEXCEEDING 30 FEET PER SECOND AND FLOWING SAID DISENGAGED VAPOROUSCOMPONENT THROUGH THE AFORESAID BED OF PARTICLE-FORM MATERIAL ININTIMATE ASSOCIATION WITH SAID LIQUID COMPONENT.
 4. AN APPARATUS FORDISTRIBUTING AMIXED PHASE FEED COMPRISING A VAPOROUS COMPONENT AND ALIQUID COMPONENET UNIFORMLY OVER A BED OF PARTICLE-FORM SOLID MATERIALWHICH COMPRISES A CLOSED CONTAINER, A MIXED FEED INLET, AN OUTLET, A BEDOF PARTICLE-FORM SOLID MATERIAL IN THE LOWER REGION OF SAID CONTAINER, ASECONDARY DISTRIBUTOR VERTICALLY SPACED UPWARDLY FROM SAID BEDPARTICLE-FROM MATERIAL CONSTRUCTED AND ARRANGED TO PROVIDE A PLURALITYOF DOWNWARDLY EXTENDING CONDUITS IN THE RATIO OF ONE CONDUIT FOR EACH0.1 TO NOT MORE THAN ABOUT 1.0 SQUARE FOOT OF HORIZONTAL CROSS-SECTIONALAREA OF SAID BED OF PARTICLE-FORM SOLID MATERIAL, A PRIMARY DISTRIBUTORCONSTRUCTED AND ARRANGED TO DELIVER IN SUBSTANTIALLY NONTURBULENT FLOWTO SAID SECONDARY DISTRIBUTOR SAID LIQUID COMPONENT WHILST DISENGAGINGAT LEAST A PORTION OF SAID VAPOROUS COMPONENT OF SAID MIXED PHASE FEED,AND MEANS FOR INTRODUCING SAID MIXED PHASE FEED, AND PRIMARYDISTRIBUTOR.